EP2026003A2 - Abfallbehandlungsverfahren und -vorrichtung - Google Patents

Abfallbehandlungsverfahren und -vorrichtung Download PDF

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Publication number
EP2026003A2
EP2026003A2 EP08018657A EP08018657A EP2026003A2 EP 2026003 A2 EP2026003 A2 EP 2026003A2 EP 08018657 A EP08018657 A EP 08018657A EP 08018657 A EP08018657 A EP 08018657A EP 2026003 A2 EP2026003 A2 EP 2026003A2
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EP
European Patent Office
Prior art keywords
waste
unit
plasma
gas
treatment
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Withdrawn
Application number
EP08018657A
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English (en)
French (fr)
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EP2026003A3 (de
Inventor
Chris Chapmann
David Ovens
David Deegan
Saeed Ismail
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Advanced Plasma Power Ltd
Original Assignee
Tetronics Ltd
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Filing date
Publication date
Application filed by Tetronics Ltd filed Critical Tetronics Ltd
Priority to EP10181311.1A priority Critical patent/EP2264367A3/de
Priority claimed from EP06755679A external-priority patent/EP1896774B1/de
Publication of EP2026003A2 publication Critical patent/EP2026003A2/de
Publication of EP2026003A3 publication Critical patent/EP2026003A3/de
Withdrawn legal-status Critical Current

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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
    • F23G5/02—Incineration of waste; Incinerator constructions; Details, accessories or control therefor with pretreatment
    • F23G5/027—Incineration of waste; Incinerator constructions; Details, accessories or control therefor with pretreatment pyrolising or gasifying stage
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B09—DISPOSAL OF SOLID WASTE; RECLAMATION OF CONTAMINATED SOIL
    • B09B—DISPOSAL OF SOLID WASTE
    • B09B3/00—Destroying solid waste or transforming solid waste into something useful or harmless
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
    • C10B49/00—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
    • C10B57/00—Other carbonising or coking processes; Features of destructive distillation processes in general
    • C10B57/02—Multi-step carbonising or coking processes
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23C—METHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN  A CARRIER GAS OR AIR 
    • F23C6/00—Combustion apparatus characterised by the combination of two or more combustion chambers or combustion zones, e.g. for staged combustion
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
    • F23G5/006—General arrangement of incineration plant, e.g. flow sheets
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
    • F23G5/02—Incineration of waste; Incinerator constructions; Details, accessories or control therefor with pretreatment
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
    • F23G5/08—Incineration of waste; Incinerator constructions; Details, accessories or control therefor having supplementary heating
    • F23G5/085—High-temperature heating means, e.g. plasma, for partly melting the waste
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
    • F23G5/30—Incineration of waste; Incinerator constructions; Details, accessories or control therefor having a fluidised bed
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
    • F23G5/44—Details; Accessories
    • F23G5/46—Recuperation of heat
    • H—ELECTRICITY
    • H05—ELECTRIC TECHNIQUES NOT OTHERWISE PROVIDED FOR
    • H05H—PLASMA TECHNIQUE; PRODUCTION OF ACCELERATED ELECTRICALLY-CHARGED PARTICLES OR OF NEUTRONS; PRODUCTION OR ACCELERATION OF NEUTRAL MOLECULAR OR ATOMIC BEAMS
    • H05H1/00—Generating plasma; Handling plasma
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2201/00—Pretreatment
    • F23G2201/30—Pyrolysing
    • F23G2201/303—Burning pyrogases
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2201/00—Pretreatment
    • F23G2201/30—Pyrolysing
    • F23G2201/304—Burning pyrosolids
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2201/00—Pretreatment
    • F23G2201/40—Gasification
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2203/00—Furnace arrangements
    • F23G2203/50—Fluidised bed furnace
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2204/00—Supplementary heating arrangements
    • F23G2204/20—Supplementary heating arrangements using electric energy
    • F23G2204/201—Plasma
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2206/00—Waste heat recuperation
    • F23G2206/20—Waste heat recuperation using the heat in association with another installation
    • F23G2206/203—Waste heat recuperation using the heat in association with another installation with a power/heat generating installation
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2900/00—Special features of, or arrangements for incinerators
    • F23G2900/50208—Biologic treatment before burning, e.g. biogas generation
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E20/00—Combustion technologies with mitigation potential
    • Y02E20/12—Heat utilisation in combustion or incineration of waste

Definitions

  • a third method for processing waste involves the gasification of the waste.
  • Gasification is the partial combustion of a material, where the oxygen in the gasification unit is controlled such that it is present at a sub-stoichiometric amount, relative to the waste material.
  • Gasification of waste containing carbonaceous components results in a combustible fuel gas rich in carbon monoxide, hydrogen and some saturated hydrocarbons, principally methane.
  • Gasification while being moderately successful in combusting the majority of waste, nevertheless produces a gas that contains uncombusted particulates, low volatility tarry species and airborne compounds. Additionally, although much of the waste is combusted to either a gas or airborne particles, the gasification process still often results in a 'char', i.e. a solid material that contains constituents that will not readily combust or vaporise under the operating conditions of the gasification. The char commonly contains hazardous heavy metal and toxic organic species, which must be disposed of carefully, adding to the cost of the overall waste treatment process. It will be appreciated that there is a desire to reduce the amount of solid waste that results from a waste-treatment process, and also reduce the amount of hazardous materials in the treated waste.
  • the present invention provides a process for the treatment of waste, the process comprising a gasification step comprising treating the waste in a gasification unit to produce an offgas and a char, and a plasma treatment step comprising subjecting the offgas and the char product to a plasma treatment in a plasma treatment unit.
  • the offgas typically will contain uncombusted solid particles and tarry species.
  • the first aspect may provide a process for the treatment of waste, the process comprising
  • a waste material having been thermally dried may have a moisture content in the range 10-16 wt%of about 12% or less: the above form I of the waste is therefore representative of thermally dried waste.
  • a waste material having been dried by a so-called 'MBT' Mechanism Biological Treatment, such as rotary aerobic digestion
  • Table 2 (Ultimate analysis of waste from Table 1 containing 25 % moisture by weight) C H O S N CI Ash (other elements) Moisture Content 36.9 4.9 24.12 0.15 0.5 0.5 8.03 24.9 100
  • the elemental amounts of H and O in Table 2 are from the theoretically dry components.
  • the process according to the present invention comprises a gasification step.
  • the gasification step may, for example, be carried out in a vertical fixed bed (shaft) gasifier, a horizontal fixed bed gasifier, a fluidised bed gasifier, a multiple hearth gasifier or a rotary kiln gasifier.
  • a horizontal fixed bed gasifier may otherwise be referred to in the prior art as a starved air combustor (incinerator), controlled air combustor, pyrolytic combustor, or a modular combustion unit (MCU).
  • a starved air combustor incinerator
  • controlled air combustor controlled air combustor
  • pyrolytic combustor pyrolytic combustor
  • MCU modular combustion unit
  • a horizontal fixed bed gasifier generally comprises two sections: a primary combustion chamber and a secondary combustion chamber.
  • waste is gasified by partial combustion under sub-stoichiometric conditions, producing low-calorific gas, which then flows into the secondary combustion chamber, where it is combusted with excess air.
  • the secondary combustion produces high-temperature (650 to 870°C) gases of complete combustion, which can be used to produce steam or hot water in an optionally attached waste boiler.
  • High-temperature (650 to 870°C) gases of complete combustion which can be used to produce steam or hot water in an optionally attached waste boiler.
  • Lower velocity and turbulence in the primary combustion chamber minimize the entrainment of particulates in the gas stream, leading to lower particulate emissions than conventional excess-air combustors.
  • a typical fluid bed gasification unit may comprise a vertical steel cylinder, usually refractory lined, with a sand bed, a supporting grid plate and air injection nozzles known as tuyeres.
  • tuyeres When air is forced up through the tuyeres, the bed fluidises and expands up to twice its resting volume.
  • Solid fuels such as coal or refused derived fuel, or in the case of the present invention, the waste feedstock, can be introduced, possibly by means of injection, into the reactor below or above the level of the fluidised bed.
  • the "boiling" action of the fluidised bed promotes turbulence and transfers heat to the waste feedstock.
  • auxiliary fuel natural gas or fuel oil
  • auxiliary fuel is usually not needed.
  • the gasification unit most preferably the fluid bed gasification unit, will be a vertical, cylindrical vessel, which is preferably lined with an appropriate refractory material, preferably comprising alumina silicate.
  • the distance between the effective surface formed by the particles of the fluid bed when fluid (i.e. when gas is being fed through the particles from below) and the top of the unit is called the "free board height".
  • the free board height in use, will preferably be 2.5-5.0 (more preferably 3.5 to 5.0) times the internal diameter of the unit.
  • This geometric configuration of the vessel is designed to permit adequate residence time of the waste within the fluid bed to drive the gasification reactions to completion and also to prevent excessive carry over of particulates into the plasma unit.
  • the gasification unit will preferably employ a heated bed of ceramic particles suspended (fluidized) within a rising column of gas.
  • the particles may be sand-like.
  • the particles may comprise silicon oxide.
  • the waste will be fed continuously to the gasification unit at a controlled rate.
  • the gasification unit is a fluid bed gasification unit, preferably the waste is fed either directly into the bed or above the bed.
  • the waste feed will be transferred to the gasifier unit using a screw conveyor system, which enables continuous addition of waste.
  • the waste feed system may incorporate an air lock device, such that the waste can be fed into the gasification unit through the air lock device to prevent air ingress or gas egress to/from the interior of the gasifier unit.
  • the waste is preferably fed through the airlock device with additional inert gas purging.
  • Air lock devices are known to the skilled person.
  • the gasification is carried out in the presence of steam and oxygen.
  • water which will be converted to steam, may be introduced into the gasification unit in the form of liquid water, a spray of water, which may have a temperature of 100°C or less, or as vapour having a temperature of 100°C or more.
  • the heat in the interior of the gasification unit ensures that any liquid water, which may be in the form of airborne droplets, is vaporised to steam.
  • the steam and oxygen will be closely metered to the unit and the rate of waste feed adjusted to ensure that the gasifier operates within an acceptable regime.
  • the amount of oxygen and steam introduced to the gasification unit relative to the amount of waste will depend on a number of factors including the composition of the waste feed, its moisture content and calorific value.
  • the amount of oxygen introduced to the gasification unit during the gasification step is from 300 to 350 kg per 1000 kg of waste fed to the gasification unit.
  • the amount of steam introduced to the gasification unit is from 0 to 350 kg per 1000 kg of waste introduced to the gasification unit, optionally from 90 to 300 kg per 1000 kg of waste or 120 to 300 kg per 1000 kg of waste, most preferably 300 - 350 kg of waste, if the waste contains less than 20% (optionally less than 18%) by weight moisture.
  • the gasification unit will preferably comprise a fossil fuelled underbed preheat system, which will preferably be used to raise the temperature of the bed prior to commencement of feeding to the unit.
  • the addition rate of oxygen and steam will preferably be in the range as indicated in Table 2 below.
  • Table 2 Typical relative addition amounts of oxygen and steam oxidants RDF 12% moisture* RDF 25% moisture* Relative oxygen addition amount (kg per 1000 kg waste) 300-350 300-350 Relative steam addition amount (kg per 1000 kg waste) 90-300 0-100 * Based on composition of waste feed (the refuse derived fuel) given in table 1
  • the maximum temperature that can be employed in the fluidised bed of a fluidised gasification unit is dependent on the composition of the ash content of the fuel being treated.
  • some biomass materials are high in potash, soda and other species that form low melting point eutectics.
  • the temperature of the fluidised bed may be maintained by controlling the amount of oxidant fed to the gasifier relative to the amount of the solid fuel.
  • the zone above the fluid bed (sometimes termed the freeboard) may be a higher temperature than the fluid bed.
  • the temperature of the zone above the fluid bed is preferably in the range of from 800-1000°C.
  • the gas produced from the gas plasma treatment is used in a turbine or gas engine to generate electricity.
  • the turbine may be a conventional boiler steam turbine or gas turbine.
  • the syngas resulting from the plasma treatment process is preferably cooled or allowed to cool to a temperature to below 200°C prior to use in a turbine. This allows the partially combusted components of the gas, e.g. carbon monoxide, to be combusted completely and efficiently.
  • the syngas from the plasma treatment is cooled using a heat exchange system which transfers the heat to another (heat transfer) gas, preferably the heat transfer gas is used to heat a steam turbine for additional power generation.
  • an electrode is located in the roof of the furnace and another electrode is located at the base of the furnace. Both electrodes are connected to a power source to enable generation of plasma within the furnace.
  • diagram (b) the same configuration as in diagram (a) is shown, with an additional start electrode (shown to the left of the furnace) to enable ease of start-up of the plasma generation system, as would be appreciated by the skilled person.
  • the graphite electrode(s) will be drilled, and a plasma stabilizing gas (eg nitrogen or argon) will be injected down the centre of the electrode(s).
  • a plasma stabilizing gas eg nitrogen or argon
  • the plasma unit may comprise one or more gas entry feed ports for the introduction of the offgas into the plasma unit; the feed ports may be located in a sidewall or the roof of the plasma unit.
  • the tar-laden gas (the offgas) from the gasifier will preferably enter the plasma unit either through a port in the sidewall or roof.
  • the plasma unit will be designed to prevent or minimise short circuiting of the dirty gas, for example:
  • the oxidant injection point will preferably be remote from the electrodes to prevent high graphite wear rates.
  • the off-gas composition will preferably be continuously monitored and a feed back control loop may be employed to adjust the power and oxidant feed rate to the plasma unit.
  • the reformed gas (syngas), which results from the plasma treatment, will preferably be further cleaned to remove acid gases, particulates and heavy metals from the gas stream to produce a fuel that can be use in the generation of electricity and heat for steam raising.
  • the plasma treatment unit will generate a solid and/or molten material, as would be know to the skilled person.
  • the process may further comprise collecting the solid and/or molten material produced in the plasma treatment unit.
  • the apparatus may further comprise a unit for the aerobic microbial digestion of waste which may be as described herein.
  • the process preferably further comprises subjecting the waste to microbial digestion, more preferably aerobic microbial digestion, prior to the gasification step.
  • microbial digestion more preferably aerobic microbial digestion
  • This has the added advantages of producing a more homogenous feedstock with a higher' calorific content and less moisture content than unprocessed waste, which allows for a much more efficient combined gasification and plasma process.
  • the gasification process is far more efficient with a feedstock of relatively consistent calorific value.
  • an efficient plasma treatment should ideally have a relatively homogenous feed of offgas.
  • the moisture content of the waste prior to aerobic digestion may be from 20 to 75 % by weight, preferably 25 to 50% by weight.
  • the waste has an average moisture level of 45 % or less, preferably 30% or less, after the aerobic digestion treatment.
  • the microbial digestion step preferably comprises the steps of:
  • the first supply of waste comprises organic waste, preferably solid organic waste.
  • the other waste may comprise solid waste.
  • Variations in the physical composition (for example calorific content) and moisture level of the first waste (typically domestic waste, but also possibly agricultural waste) can be 'smoothed out', so that a product formed from treated waste from different areas or different time periods can be relatively homogeneous.
  • the waste, either the first and/or the other waste, treated using the microbial step is preferably "organic waste", preferably solid organic waste, for example domestic waste, industrial waste or agricultural waste.
  • Organic waste is waste that has at least a proportion of organic material capable of being treated microbially.
  • the other waste mixed with the first waste preferably also contains organic material.
  • the microbial digestion step will preferably produce heat. This breakdown is accelerated by changes in the physical nature of the waste.
  • the microbial activity is bacterial activity.
  • the microbial activity is aerobic.
  • thermophilic phase which normally occurs in the temperature range 60°C - 75°C, most preferably around 63°C - 70°C. In this phase, very rapid digestion occurs with the production of heat. It is found that the reaction in the thermophilic phase is much quicker than the commonly used mesophilic phase which occurs in the range 30°C - 38°C.
  • thermophilic phase results in the natural generation of heat which breaks down the waste to produce a material which is suitable for processing to provide a fuel or compost.
  • the microbial reaction will almost always provide sufficient heat to maintain itself without provision of supplementary heat.
  • chemical mixing of the waste can lead to an increase in temperature which assists the commencement of the microbial activity.
  • Other material may be added to the microbial treatment vessel, for example quicklime, to control pH.
  • the oxygen content (and, optionally moisture level) of gas removed from the treatment vessel is measured. This is a particularly convenient arrangement.
  • the gas in the microbial treatment vessel will typically comprise atmospheric nitrogen, oxygen, carbon dioxide and water vapour. This gas may contain no methane, ammonia or hydrogen sulphide, as the microbial activity is carried out in the thermophilic phase.
  • air or oxygen can be supplied to the treatment vessel.
  • Air or oxygen can be supplied continuously throughout at least part of the process or in discrete inputs of air/oxygen.
  • the moisture level in the gas in contact with the waste in the microbial treatment vessel is maintained at a level below its dew point. This ensures that water is-substantially continuously removed from the waste being treated into the gas space by evaporation.
  • the flow of air and gas through the microbial treatment vessel also removes heat from this part of the apparatus. It is found that an adequate heat balance can be achieved. That is, heat generation by the microbial activity within the concentrated mass of waste can be balanced with heat removal by the gas flowing through the vessel so that the temperature is maintained at a desirable level.
  • the drum preferably comprises a substantially parallel sided circular section cylinder.
  • the axis of the cylinder may be inclined to the horizontal, for example at an angle in the range 3° - 10° most preferably 5° - 8°, to provide gravitational flow through the drum.
  • Average residence time of the waste in the microbial treatment vessel is suitably in the range 18-60 hours, more preferably around 24 to 48 hours, most preferably around 36 hours.
  • the second parameter which may be controlled is the average moisture content of at least some of the waste treated in the microbial treatment step.
  • the average moisture level of this part of the waste is suitably in the range 20-75%, more preferably 30 to 60%, most preferably 30 to 50%.
  • Moisture levels of waste may be measured by measuring the moisture level of air or gas over the waste at a fixed temperature and in equilibrium with it.
  • the moisture level of waste fed to the digester may'be manipulated by altering the mixing ratios of different types of waste.
  • at least part of the waste fed to the microbial digester has a moisture level in the range 20-75% by weight, preferably 25 to 65% by weight in order to promote the faster thermophilic reaction.
  • part of the waste fed to the digester may comprise a relatively dry commercial waste.
  • the heat generated by the digestion of the moist waste is sufficient to treat the whole of the waste fed to the treatment vessel.
  • the commercial and domestic waste are slowly mixed together reducing the overall moisture content of the mixture, so that at the end of the processing, the moisture level does not exceed 45% by weight and preferably does not exceed 25% by weight.
  • the waste in the microbial treatment step it is desirable to produce a product which is substantially homogeneous, such that its constituents are particles have a relatively small size distribution, the particles have a largest measurement of 50 mm or below.
  • the blending step helps to improve the homogeneity of the product.
  • the density of the waste fed to the microbial treatment vessel is suitably not too low.
  • the density is not less than 450g per litre, preferably not less than 750g per litre.
  • the blending step is particularly useful here.
  • Domestic waste can have a relatively high density.
  • the average density can be controlled by admixing a suitable quantity of commercial waste, which has a comparatively low density.
  • the waste In order to convert the treated waste to fuel, the waste may be classified according to size and subsequently densified to provide pellets of suitable size for use in the gasification step. During this pelletisation stage, further drying of the waste may occur, due to heat generation caused by friction and due to further exposure to air.
  • the moisture level of the treated material is in the range 10-25% by weight.
  • Figure 5 shows:
  • the FBG uses a heated bed of alumina silicate ceramic particulates as the bed media.
  • RDF (refused derived fuel) feedstock is fed continuously, at a controlled rate, to the FBG 1 through a solid fuel feeder system.
  • the as-received feed is transferred by a belt conveyor 2 to a surge hopper 3 where a variable-speed screw conveyor controls the volumetric feed rate of the solids. These discharge into an airlock.
  • a constant speed screw conveyor is employed to transfer the feed from the airlock to the fluidised bed 1 where it is charged above the upper surface of the bed Additional inert gas purging is used at the hopper and at the airlock to prevent air ingress or gas egress into the feed stream.
  • Oxygen is supplied from a 'Titan' multi-pack of 10-11 cylinders.
  • the flow rate is controlled through a mass flow controller (MFC) rated up to 500 Nlpm.
  • MFC mass flow controller
  • the dirty offgas from the gasifer flows via a refractory lined duct to the plasma converter. Additional oxygen and steam is axially injected into the gas stream at the point of entry into the converter.
  • the high temperature and addition of oxidants at the converter stage promotes the cracking and reforming of organic species and gasification of sooty and char products.
  • the power to the plasma arc is controlled to maintain a temperature of gases exiting the unit to - 1000-1300°C. Ash particulates that are carried over from the gasifier will drop out and be assimilated in the melt. After treatment in the converter unit the syngas exits via a second gas port in the base of the unit.
EP08018657.0A 2005-06-29 2006-06-29 Abfallbehandlungsverfahren und -vorrichtung Withdrawn EP2026003A3 (de)

Priority Applications (1)

Application Number Priority Date Filing Date Title
EP10181311.1A EP2264367A3 (de) 2005-06-29 2006-06-29 Abfallbehandlungsverfahren und -vorrichtung

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
GB0513299A GB2423079B (en) 2005-06-29 2005-06-29 Waste treatment process and apparatus
GB0604691A GB2422602B (en) 2005-06-29 2006-03-08 Combined gasification and plasma treatment of waste
EP06755679A EP1896774B1 (de) 2005-06-29 2006-06-29 Abfallbehandlungsverfahren und -vorrichtung

Related Parent Applications (1)

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EP06755679A Division EP1896774B1 (de) 2005-06-29 2006-06-29 Abfallbehandlungsverfahren und -vorrichtung

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